1. Introduction - Firenze University Press

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the case of the drying of the fuel in the same range of oxygen recovery ratio stream of coal decreases from 156 kg/s to 136 kg/s. As a result of the process of producing technical oxygen in the air separation unit based on three - end type high-temperature membrane in comparison with the classic coal boiler, a significant reduction in thermal efficiency of the boiler can be observed. The results of the analysis of the impact of the oxygen recovery ratio in the membrane on the boiler thermal efficiency are shown in figure 4. In the variant without drying of the fuel for the oxygen recovery ratio equal to 0.45 boiler thermal efficiency is only 63.6%. When drying of the lignite was implemented, for the same oxygen recovery ratio thermal efficiency of the boiler increased by over twelve percentage points, to 75.8%. Fig. 4. Boiler thermal efficiency as a function of the oxygen recovery ratio in the membrane. For the variant with fuel drying, despite a higher LHV of fuel for low volumes of recovery of oxygen recovery ratios in the membrane, the boiler thermal efficiency increases with the oxygen recovery ratio up to the value of 86.8%. For the oxygen recovery ratio equal to 0.9 in the variant with fuel drying an increase in thermal efficiency of the boiler compared to the variant without drying by six percentage points was observed. Summary This paper presents a model of the supercritical circulating fluidized bed OXY type boiler integrated with the air separation unit based on three - end type high temperature membrane and the installation of fuel drying and results of studies of the impact of lignite drying on a number of characteristics, such as mass flow of fuel supplied to the boiler and boiler thermal efficiency. A sensitivity analysis of a built model shows that a change of oxygen recovery ratio at a high temperature membrane causes an increase in thermal efficiency of the boiler. For oxygen recovery ratio from 0.45 to 0.9 for the installation with a working lignite dryer, the boiler thermal efficiency increases from 75.8% to 86.8%. The increase in thermal efficiency of the boiler in comparison to the installation without lignite dryer ranges from 12 percentage points for the oxygen recovery ratio equal to 0.45 to 6 percentage points for the oxygen recovery ratio equal to 0.9. Basing on the outcome results it can be concluded that the fuel drying in OXY type systems fed by lignite leads to a significant increase in the boiler thermal efficiency. In addition to an increase in efficiency, the use of fuel drying leads to a reduction of water stream supplied to the system and thus helps to reduce the likelihood of condensation of moisture from the exhaust gases. 203
Acknowledgements The results presented in this paper were obtained from research work co-financed by the National Centre for Research and Development within a framework of Contract SP/E/2/66420/10 – Strategic Research Programme – Advanced Technologies for Energy Generation: Development of a technology for oxy-combustion pulverized-fuel and fluid boilers integrated with CO2 capture. References [1] Chmielniak T., Kosman G., ukowicz H., Integracja instalacji wychwytu CO2 z kondensacyjnymi blokami energetycznymi. Rynek Energii, 2008, 6 (79), 75-8<strong>1.</strong> [2] Pfaff I., Kather A.: Comparative thermodynamic analysis and integration issues of CCS steam power plants based on oxy-combustion with cryogenic or membrane based air separation. Energy Procedia, 1 (2009), 495-502. [3] The technical report of step 6.1 in research topic: "Numerical simulations and systemic analysis of oxy - burning," the research task 2 " Development of a technology for oxy-combustion pulverized-fuel and fluid boilers integrated with CO2 capture." in the strategic program of research and development, "Advanced Technologies for Energy Generation ". [4] Skorek – Osikowska A., Bartela .: Model of a supercritical oxy-boiler - analysis of the selected parameters. Rynek Energii, 2010, 5 (90), 69 – 75. [5] Castillo R.: Thermodynamic analysis of a hard coal oxyfuel power plant with high temperature three-end membrane for air separation. Applied Energy, 88 (2011), 1480-1493. [6] Stadler H. et al.: Oxyfuel coal combustion by efficient integration of oxygen transport membranes. International Journal of Greenhouse Gas Control, 5 (2011), 7-15. [7] Liszka M., Zibik A.: Coal – fired oxy – fuel power unit – Process and system analysis. Energy, 35 (2010), 943 – 95<strong>1.</strong> 204
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Proceedings e report 90
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ECOS 2012 : the 25 th International
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Advisory Committee (Track Organizer
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The 25 th ECOS Conference 1987-2012
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VOLUME VI CONTENT VI. 1 CARBON CAPT
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-----------------------------------
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» Personal transportation energy c
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» Excess enthalpies of second gene
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VOLUME IV IV . 1 - FLUID DYNAMICS A
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» Exergy analysis and genetic algo
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» Optimal lighting control strateg
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» Stability and limit cycles in an
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PROCEEDINGS OF ECOS 2012 - THE 25 T
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Fig. 2. The exergy destruction of M
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ineffectiveness of the catalyst, in
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[ P EXmth EX SNG] ESR F where EXm
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Fuel inputkW 728221 203771 237719 3
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Not only at desined Rc (the ratio o
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4. DISCUSSION The graphic exergy an
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Figure 9(a) illustrates the energy
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Engineering Technical Conferences &
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generally there are four kinds of m
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However, even under the off-design
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Fig. 3. 600MW supercritical coal-fi
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CO2 rich loading(molCO2/molMEA) 0.4
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Net efficiency (%) 40.28 30.29 26.4
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Fig. 11. Schematic diagram of heat
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28.67%. In addition, through heat i
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Applied Thermal Engineering 2010;30
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Abstract: PROCEEDINGS OF ECOS 2012
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Fig. 1. Solution diagram of „four
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K ~ K 1 eK 1a p K 1a iK mK
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Oxygen recovery rate, % 105 95 85 7
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Calculated optimal compressor press
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The net amount of the flue gas leav
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Figure 3. Idea for lignite drying b
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Energy efficiency, % 34,00 33,00 32
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points efficiency increase related
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Figure A1b. Thermoflex flow sheet o
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Figure A3a. Thermoflex flow sheet o
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Figure A4. Thermoflex flow sheet of
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2.1. Life Cycle Assessment 2.1.1. G
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these factors. A sensitivity analys
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methane slip contributes to 13% of
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As can be seen in Fig. 5 the impact
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References [1] Eurobserv’er, The
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in which CO2 is separated from H2,
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dimensions of water droplets and wa
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Temperature (°C) 8 7 6 5 4 3 2 1 0
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4. Conclusions In the present paper
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penalty, but without separate captu
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0.5 - 0.7 kg/kg, resulting typicall
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3.3 - Utilising waste heat All exis
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4.5 - Suomusjärvi olivine deposits
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material will change from a few % t
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Fig. 5 Schematic diagram of the PFB
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8. Combined SO2 capture and CO2 min
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Fig. 10 Carbonate- (left) and sulph
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[13] Ekdahl, E., Idman, H. Statemen
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HEAT Fig. 1. Scheme and main reacti
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(raw) materials pre-heating and AS
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Fig 3- Aspen Plus® model 110
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Table 4. Elemental and XRD analysis
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the ÅA CSM route. The content of M
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moisture - 0,2237 ash - 0,0876 LHV
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2.2 CFB plant For the current momen
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The CO2 emission factor which indic
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The CO2 emission factor calculated
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Appendix A Fig A.1. Simulation mode
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(b) Fig. A.2. Simulation model of C
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Table A.1. Calculated parameters at
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References [1] Pfaff I., Oexmann J.
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with a CC installation could be avo
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2.3. Basic CHP plant indices. The b
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3. Off-design calculations The main
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Fig. 6. CHP plant efficiency Fig. 7
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amount of steam delivered to the he
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[5] Lukowicz H., Mroncz M.: Analysi
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water removal is feasible by coolin
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Figure 2. Sketch of the suggested P
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a b Figure 5. a) Exergy balance of
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Page 181 and 182: Figure 7a. Impact of S/CATR on PCU
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Page 187 and 188: 3.1. JACOBIAN-ASPEN Interface ASPEN
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Page 219 and 220: Concerning the absorption reaction,
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Page 225 and 226: systems for fuel drying waste strea
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Page 235 and 236: N 1 i ( x x i n 1 m ) 2.3. Carbon
Page 237 and 238: DTA analysis of the untreated APCrs
Page 239 and 240: Table 4. Relative Error (%) of the
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Page 243 and 244: [1] M. Fernández Bertos, S.J.R. Si
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Page 253 and 254: Table 6. Experimental conversions o
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Page 275 and 276: Table A2. Extraction equations and
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Tabel 1. Characteristics quantities
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N m eT 4a ~ T cp T4a 1 ( K
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Auxiliary power rate of ASU, % 40 4
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[8] Buhre B.J.P., Elliott L.K., She
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1.1 - Cement Manufacturing The ceme
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2. Numerical model The purpose of t
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-0.309x15.77x2 2.085x3 240x4 12.53x
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Table 4 - Results of the optimizati
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1. Define the studied system (in th
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cycle) or a lignin extraction plant
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limiting factor for the maximum siz
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Table 5. Key data for the four ener
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Global CO 2 emissions [ktonnes/yr]
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for biofuels and the investment cos
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The possibility to capture CO2 from
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[17] Berglin N, Andersson L. Proces
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Therefore NL Agency (an agency of t
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2.2.2. Pinch analysis Pinch analysi
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3. Case study 3.1. Plant and proces
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Te 1000 mp era 900 tur 800 e [°C 7
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Application of the approach led to
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The advantage of dynamic models is
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e equal at both time intervals and
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2.5. Selecting the number of TSs Se
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A) Time Slices for solar thermal en
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The first step of procedure is to p
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cTSs demand TS solar TSs 0 2 4 6 8
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In the presented paper a framework
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[5] Erdil E, Ilkan M, Egelioglu F.
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district energy network simulation
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were decreased by 10°C.All scenari
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Site 3 Heat sources Heat load Site
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3.2.2. Input data and assumptions A
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Fig.7 shows the operation forecast
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[13] TERMIS Operation User Guide, 7
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Polygeneration is a term used to de
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The increase in energy utilization
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are available for an entire year, 8
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6. Extensions to core methodology 6
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thermal storage and possible suppor
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laterites. Ore Geology Reviews, v.
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gasification [15], hybrid biomass g
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the second reactor. In this unit, s
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The variables effect was evaluated
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atio, as well as the shift-syngas f
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Fig. 4. Effect of operating tempera
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SDG has slight effect on the syngas
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[26.] Castle WF. Air separation and
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1. Introduction - Firenze University Press

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